ES2295258T3 - PROCEDURE FOR LITTLE CORROSIVE AND POOR COINCINERATION IN HIGHLY HALOGENED WASTE EMISSIONS IN WASTE INCINERATORS - Google Patents

Abstract

Procedure for the low corrosive and poor co-incineration of highly halogenated liquid waste in waste incinerators, in which the waste incinerator contains at least one combustion chamber (3), a recovery boiler (5), a gas washing multi-stage smoke formed by an acid wash (7) and an alkaline wash (8), characterized in that sulfur or a suitable sulfur carrier is dosed in a regulated manner depending on the total halogen load and of the halogen type.

Description

Procedure for little co-incineration corrosive and poor in highly halogenated waste emissions in waste incinerators.

The invention relates to the little co-incineration corrosive and poor in highly halogenated waste emissions, preferably of liquid waste, in an incinerator of waste. Already partly during combustion, and then in greater measured when the cooling of the flue gas in the boiler begins next, unwanted free halogens are formed, such as, by example, free chlorine Cl 2, free bromine Br 2 and / or free iodine I_ {2}. The subsequent formation of free halogens, dependent on temperature and kinetically limited, from corresponding hydrogen halides follow the so-called Deacon's reaction, which, fortunately, is strongly inhibited By adding regulated sulfur, that is, adapted to the corresponding total halogen charge, to the chamber of combustion of the waste incinerator and the SO_ {2} formed to from it as a result of the incineration it is possible to suppress much of these free halogens still in the boiler, is that is, on the path that the smoke gas travels until the end of the boiler

In H.W. Fabian et al. [1], for example, describes a waste incinerator. Waste incinerators  typical contain a primary combustion chamber (for example a rotary tubular furnace), a secondary combustion chamber (post-combustion chamber), a recovery boiler, sometimes also an electrostatic or filter dust separator, a wash of smoke gas with, for example, acid washing of one or more stages (sudden cooling and, for example, acid rotary washer-sprayer) and washing alkaline (for example rotary washer-sprayer alkaline), if necessary also with a drop collector and, for example, an electrostatic condensation filter.

During the incineration of waste with Halogen content is generated by hydrolysis in the chamber of combustion predominantly predominantly halides of hydrogen, such as HCl, and to a lesser extent also halogens free, as well as traces of radicals and halogen atoms initially not fixed. When the smoke gas cools, the latter They recombine to give free halogens. Additionally they form a from hydrogen halides, especially in the presence of volatile ashes rich in metal oxides that act as Deacon reaction catalysts (4 HX + O2) 2 2 X 2 + 2 H 2 O, with X = Cl, Br or I), increasingly free halogens, such as chlorine Cl2. The dimensions of this subsequent formation of free halogens according to the catalyzed Deacon reaction also depends on the type and the amount of volatile ashes present in the boiler.

There are many reasons why you don't want to halogen free.

- Unlike hydrogen halides, the free halogens are insoluble in the acid wash zone and they can only be leached in the alkaline wash by chemo absorption with, for example, caustic soda (NaOH) in the form of halide of sodium and sodium hypohalogenide in the same proportions.

- The concentration of hypohalogenide in water of alkaline washing should be kept low by a contribution enough of reducing agents, that is, should be reduced to stable sodium halide by, for example, hydrogen sulphide or thiosulfate to avoid free halogen emissions along with the pure gas When the contribution of reducing agents is insufficient there is a risk that the limit values are not met established by law in pure gas after gas washing smoke.

- Higher concentrations of free halogens in Boiler smoke gas can corrode the boiler, as well as also the rest of the installation.

- Free halogens favor the so-called de novo synthesis of dioxins and furans in the central and posterior areas of the boiler, as well as, where appropriate, in an electrostatic or filter dust separator arranged directly after the boiler.

Suppressing free chlorine and / or other halogens free via SO_ {2} can be deleted, or at least limited strongly, the undesirable effects described above, such as the new formation of dioxins and furans [1], see [2], [3], [4].

It is known that free halogens react with SO_ {2} still in the boiler. Free chlorine, for example, reacts with SO2 and water vapor under the formation of SO3 to re-give hydrogen chloride (see, for example, [1] in relationship with the deletion of Cl_ {2}). Also free bromine reacts with SO2 (see [5]); presumably, however, this reaction between Br 2 and SO 2 does not lead directly to hydrogen bromide but first, in the boiler, to SO 2 Br 2 (sulfuryl bromide) which is then hydrolyzed to HBr and SO 4 2- in the acid wash. In the case of the incineration of highly halogenated waste is not known until now exactly what proportions of the corresponding halogen charge are temporarily present in the boiler smoke gas in the form of free halogens X 2 (for example in the form of Cl 2 and / or Br 2); only known, according to the variation of the thermodynamic equilibria of the corresponding "reaction of Deacon "depending on the temperature, which in the case of bromine and iodine tends to form a much more proportion later high halogen free than in the case of chlorine.

According to Fabian et al. [1], the relationship quantitative between sulfur and chlorine in the incinerated waste menu  should be such that a "sulfur / chlorine molar ratio > 1 ". However, it was not known in detail how much "chlorine" (refers to free chlorine) was present temporarily in the flue gas of the boiler as magnitude of molar reference in the case of total variable chlorine loads. The same uncertainties existed and continue to exist also in the case of the other free halogens, such as, in particular, Br 2 and I_ {2}. In the waste incinerator of [9] it is intended achieve a sulfur / chlorine molar ratio of 1.0.

It is also known that free halogens (practically insoluble in the strongly acidic washing zone and, therefore, not leachable in it), such as Cl_ {2} and / or Br2, only dissolve with residual SO2 (also practically insoluble in the strongly acid washing zone) from raw boiler gas before abrupt cooling in the alkaline scrubber by next joint chemo absorption and it then set stably in the form of, for example, NaX, to know, by reduction of unstable NaOX hypohalogenide, formed initially along with NaX in chemo absorption, to give NaX stable, see [6].

Finally it is also known that this reduction of NaOX to stable NaX can not only be carried out using sulfur of hydrogen that is formed during the process from SO2 Residual chemo absorbed at the same time in the alkaline scrubber, but also by an external reducing agent fed into the alkaline scrubber, such as thiosulfate (Na 2 S 2 O 3 * 5H 2 O), see [7].

The measures known so far in the state of the technique and applied in waste incinerators are not sufficient for reliable suppression and / or fixation and at the same time economic of free halogens formed in the incineration of highly halogenated waste. As a consequence of alterations Selective menu of waste and operational oscillations are they frequently obtain variable total loads of halogens. Yet This requires adequate measures for the addition of service always optimally adapted to the current total load of halogens and optimized free halogen suppression correspondingly with regard to costs, especially in the case of high total halogen loads.

The objective according to the invention is, by therefore, find a procedure for the little co-incineration corrosive and poor in highly halogenated waste emissions in waste incinerators, with a minimum consumption of materials service and a minimum production of recycled materials.

The objective according to the invention is reaches with a procedure and a device for co-incineration  little corrosive and poor in emissions of liquid waste highly halogenated in waste incinerators with at least one chamber of combustion, a recovery boiler and a flue gas wash (formed, for example, by an acid wash of one or several stages and an alkaline wash), dosing in a regulated manner in the chamber of combustion, in addition to other sulfur-containing waste, solid or liquid sulfur or corresponding sulfur carriers, as, for example, waste sulfuric acid. The regulation of dosage of sulfur or sulfur carriers corresponding is done essentially proportionally to the total current load of halogens (for example at the total charge of chlorine and / or bromine) present in the smoke gas and depending on the type Halogen

Sulfur can be added directly to the primary or secondary sulfur-shaped combustion chamber solid, liquid sulfur or in the form of another sulfur carrier, such as, for example, waste sulfuric acid.

Solid sulfur is preferably added in pelletized or granulated form. This form of addition presents the advantage of pelletized or granulated solid sulfur (for example the so-called sulfur granulate) is safe in handling and easy of dosing, better than, for example, sulfur flower powder. He sulfur granulate is preferably added by feed pneumatic in the primary combustion chamber. The feeding of sulfur granulate should be done with a dosing device and adjustable conveyor, such as an endless screw of dosage or a vibrating feeder. A screw without frequency dosing end adjustable with an injector next and a pneumatic transport pipe directed towards the combustion chamber, preferably towards the furnace head swivel tubular ("insufflation of sulfur granules"). He waste sulfuric acid is added to the combustion chamber primary or secondary by means of a dosing pump adjustable to through spray nozzles or windscreens corresponding.

Other wastes containing sulfur as well such as solid or liquid sulfur or the dosed sulfur carrier in a regulated manner, they are incinerated in the primary combustion chamber and / or secondary under the formation of SO_ {2}.

Starting from the current total halogen load present in the flue gas, the dosage of sulfur or others Sulfur carriers in the combustion chamber must be regulated according to the invention such that it is maintained constantly a theoretical SO_ {2} content calculated in the gas of smoke in front of the boiler or, alternatively, a content corresponding theoretical SO2 residual in the gross gas of boiler before sudden cooling.

Sulfur or the sulfur carrier dosed from regulated form should increase sufficiently but not in excess the contribution of SO_ {2} in the flue gas of the boiler. Demand for SO_ {2} required for both suppression of free halogens in the boiler as well as for the reduction of hypochloride in the Next alkaline wash grows with the total halogen load, it is say, that the content of SO_ {2} needed in the smoke gas in front of the boiler (behind the afterburner) and / or the corresponding residual SO2 content in the gross gas of boiler behind the boiler (before abrupt cooling) must increase together with the total halogen load. The proportion of free halogens in the total halogen charge is considerably higher in the case of bromine or even iodine than in the case of chlorine, so is the demand sulfur specific, that is, the one referring to the total load of halogens in the smoke gas.

Through operational tests of "balances of chlorine and sulfur "it was determined that in the boiler smoke gas of a typical waste incinerator (which works with contents in oxygen of, for example, 11% in vol. of O 2 tr. and contents in water vapor of, for example, 10 ... 30% in vol. of H 2 O tr.), approximately 4% of the total chlorine charge is released subsequently, as the cooling of the smoke gas progresses,  in the form of free chlorine Cl 2 from hydrogen chloride through the so-called Deacon reaction for chlorine (4 HCl + O_ {2} \ leftrightarrow 2 Cl_2 + 2 H2O). Of this 4% of free chlorine subsequently formed, approximately 75% (which equals approximately 3% of the total chlorine charge) becomes to be transformed, still in the boiler, into HCl with SO2 and steam of water by the reaction of Griffin Cl 2 + SO 2 + H 2 O → 2 HCl + SO 3. So, if the contribution of Sulfur is sufficient, approximately 99% of the total load of Chlorine reaches the sewage from the acid wash directly in Water soluble HCl form. Therefore, only approximately 1% of the total chlorine load reaches the wastewater of the following alkaline wash in the form of free chlorine Cl2. There, the free chlorine Cl_ {2} is chemo absorbed together with the SO_ {2} and, if the contribution of SO_ {2} from the gross boiler gas before of abrupt cooling is sufficient, it is reduced to chloride sodium

From operational tests and balances corresponding to the case of bromine it was determined that the proportion of free bromine Br 2 subsequently formed in the gas of boiler smoke from a waste incinerator (which works with oxygen contents of, for example, 11% in vol. of O_ {2} tr. and water vapor contents of, for example, 10 ... 30% in vol. of H 2 O tr.) is much greater than that of chlorine: The proportion of Br_ {2} was not in just 4% of the total load of halogens (see chlorine), but between 40% in the case of charges total bromine lower and 65% in the case of total loads of Very high bromine.

In the case of bromine these balances demonstrate that up to> 90% of the free bromine is still suppressed in the boiler if the contribution of SO_ {2} is sufficient, probably by means of formation of sulfuryl bromide SO2 Br2 according to the reaction equation SO_ {2} + Br_ {2} \ leftrightarrow SO_ {2} Br_ {2}. In any case, operational tests made by the authors with total bromine loads both reduced as very high gave the result, unknown until now, that a reaction product is already formed in the boiler, probably this SO_ {2} Br_ {2} that at the moment is not yet can be detected directly, which, as shown, is Hydrolyzes HBr and SO4 2- in the acid wash zone. If he contribution of SO_ {2} in the smoke gas is sufficient, also in the In case of bromine, approximately 99% of the total load of Halogens in the form of HBr bromide in the wash sewage acid. Also in this case, similar to chlorine, only approximately 1% of the total halogen charge arrives in the form of Br 2 to the alkaline wash water, in which chemo absorbs and, if the residual SO_ {2} contribution is sufficient, it is reduced to NaBr stable.

Thus, the halide load in the waters acid residues constitutes, at least in the state of stationary operation, a good measure of the total load of halogens present in the flue gas of the boiler, since when the admission is constant, the total halogen charge in the smoke gas from the boiler is, if the sulfur intake is sufficient, both in the case of chlorine and also in the case of bromine in approximately 99% identical to the halide load in the waters residual acid wash.

In the non-stationary operating state on the other hand, that is, when the charges change rapidly, the halide load momentarily discharged with the waters Acid residuals from abrupt cooling just slowly follow the total current load of halogens in the flue gas of the boiler, that is to say, that appears with delay in the residual waters of the abrupt cooling, namely, with a temporary delay corresponding to the average residence time of the wash water in the acid wash sludge (order of magnitude: for example 45 min)

The concentration of halides in the waters Acid residuals are obtained, for example, by measuring the conductivity. It is known that the electrical conductivity of solutions aqueous halides strongly depends on the temperature; by this reason is integrated into the conductivity measurement a Temperature measurement to compensate for temperature. Load of corresponding halides in acidic wastewater is obtains later by multiplication of the concentration of halides by the measured acid wastewater flow, for example, by means of an inductive flowmeter.

As an alternative to indirect determination described of the total halogen charge in the smoke gas as Halide loading in acidic wastewater is also could determine directly, but comparatively expensive, the total current halogen load in the smoke gas from the contents of HX and X_ {2} in the raw boiler gas and from of the flow of smoke gas or of a magnitude proportional to the flow of smoke gas, such as the specific vaporization of the boiler; for this, the contents of HX and X_ {2} in the gas should be measured boiler gross before abrupt cooling, for example with measuring devices based on infrared spectrometry next.

To always cover the demand for sulfur with respect to the current total halogen load without providing sulfur unnecessary, it is recommended first for the mass flow of sulfur to be dosed a "primary regulation circuit which uses a sulfur dosing ramp found previously and Operationally. "In this primary regulation circuit, the residual SO2 content measured continuously in the gas boiler gross before abrupt cooling (behind the boiler) serves as "adjusted controlled magnitude" (see more ahead).

As explained, free halogens intermediates are not always completely suppressed in the boiler, to know, in the case of chlorine, for example, only in approximately 75% The remaining 25% of free chlorine reaches alkaline wash If there are no other reducing agents added external, therefore, certain content is always required residual of SO2 in the gross boiler gas before abrupt cooling (behind the boiler) to facilitate in the sufficient alkali wash internal bisulfide as agent reducer.

It is known that the bisulfide formed in the process a from the residual SO2 of the gross boiler gas in the scrubber alkaline is not stable to oxidation, that is, it not only serves for the desired reduction of hypochloride (NaOCl) but at the same time also reacts with dissolved oxygen. Residual content  of SO 2 needed in the case of chlorine in the raw gas of boiler before abrupt cooling is therefore considerably greater than it would be, from the point stoichiometric view, to the residual load of Cl2 chemoadsorbed in alkaline washing. This knowledge leads to concept of a specific "sulfur dosing ramp" of the installation, to be determined previously in tests operational for the theoretical value of the residual content of SO_ {2} in the gross boiler gas before abrupt cooling depending on the current total chlorine load (kg of Cl_ {tot} / h) and / or, when this charge refers to the flow of dry smoke gas, of the corresponding Cl_ {tot} concentration in the gross gas of boiler (mg of Cl_ tot / Nm3 tr.).

In the case of chlorine, for example, the ramp of Sulfur dosage can be determined operationally from the as follows: An "operational test with a load" is performed total elevated chlorine previously selected, "which begins with a contribution of sulfur in principle very excessive and, for consequently, a very excessive residual content of SO2 in the gross boiler gas before abrupt cooling (behind the boiler). Consequently, a principle is also obtained in considerable contribution of bisulfide in the alkaline scrubber; in this, on the other hand, there is no hypochloride and, correspondingly, in principle no free chlorine is detected in the pure gas after alkaline wash Then the sulfur intake is gradually reduced until free chlorine can be detected in pure gas. Load total chlorine previously selected and / or the corresponding Cl_ {tot} concentration previously selected in the raw gas of boiler (mg of Cl_ tot / Nm3 tr.) on the one hand, and the corresponding residual content of SO2 thus found in the gas boiler gross and allows to detect substantially free chlorine on the other, they form a point on the sulfur dosing ramp.

In principle this single point is enough to establish a sulfur dosing ramp as a ratio between the total chlorine load and / or the concentration of Cl_ {tot} in the smoke gas on the one hand and the minimum value necessary for the residual content of SO2 measured continuously in the gas boiler gross before abrupt cooling (behind the boiler) on the other, since the sulfur dosing ramp is the line that passes through this single measured point and the origin of coordinates Therefore, the line thus found indicates with sufficient accuracy and for a wide range of chlorine charges what theoretical residual content of SO_ {2} should be maintained in the gross boiler gas before abrupt cooling (behind the boiler) at different total chlorine loads so that in the wash Alkaline is always present enough bisulfide and produced in it the desired reduction of hypochloride so that it is no longer find free chlorine Cl 2 in the pure gas after washing alkaline or just a concentration of Cl2 in the minimum pure gas less than a predetermined limit value.

You can also determine a ramp of corresponding specific sulfur dosage of the installation for the dosage of sulfur in the case of bromine or iodine.

As a result of "SO_ {2} consumption" in the boiler the content of SO_ {2} (not measured operationally) in the smoke gas in front of the boiler must be clearly higher to the residual content of SO2 (measured continuously Operationally) in the gross boiler gas before cooling abrupt (behind the boiler). The determination of the difference, that is, of the consumption of SO2 attributable to the halogens in the boiler can be carried out by calculation: For the calculation in the If chlorine is to be multiplied, for example, the total load current chlorine (and / or the corresponding chloride load in the acid wastewater) by the degree of transformation of Cl2 specific to the installation in the boiler (for example 3% of the total chlorine load, namely 75% of a total of 4%), this value is then divide by the molecular mass of Cl2 (70,014 kg of Cl_ {2} / kmol) and finally it has to be multiplied by the mass Molecular Sulfur Dioxide (64.06 kg S / kmol). This consumption of calculated SO2, attributable to chlorine, which is produced in the boiler must now add to the residual demand of SO_ {2} corresponding to the total chlorine load according to the ramp of sulfur dosage. Finally, it must also be taken into account the consumption of SO_ {2} through the known and inevitable conversion oxidative of SO2 / SO3; in waste incinerators with less than 11% in vol. of oxygen this represents approximately 8% of the total SO_ {2} load. Therefore, the content of SO_ {2} found so far in the smoke gas in front of the boiler it must be increased by the corresponding factor 1 + 0.08 / 0.92 = 1.09. The theoretical SO_ {2} content thus calculated in the gas of smoke before the boiler and / or the corresponding mass flow of Sulfur is sufficient for both the partial suppression of free chlorine inside the boiler as for the reduction of hypochloride in the circulating water of the alkaline wash.

In the case of bromine, you can proceed correspondent. In this case the total bromine load is multiplied in the smoke gas and / or bromide load in wastewater by the proportion of specific intermediate free bromine of the installation and determined in the case of bromine. According to the essays of the authors, this proportion amounts to 40% for total bromine loads low and up to 65% for total loads of high bromine, and is thus much higher than in the case of chlorine. To the unlike free chlorine, free bromine reacts with SO2 largely still in the boiler (presumably to give SO_ {2} Br_ {2}), namely> 90%. It can start from a approximate degree of transformation of Br_ {2} in the boiler 100% For this calculation, the total intermediate load of Br 2 by the molecular mass of Br 2 (159.88 kg of Br 2 / kmol) and multiplied by the molecular mass of the dioxide of sulfur (64.06 kg of S / kmol). With a corresponding increase by factor 1.09 as described above is taken into account also in this case the sulfur consumption attributable to the conversion oxidative of SO2 / SO3.

The alternative procedure described in the present regulation memory with a SO_ {2} content theoretical calculated online in the smoke gas in front of the boiler as "adjusted theoretical value" of a regulation circuit primary is always interesting when you don't want to cover the demand of reducing agent necessary in alkaline washing for reduction of hypohalogenides by residual SO2 from the gross boiler gas before abrupt cooling, but by an oxidation stable external reducing agent, such as thiosulfate. In this case the ramp of Sulfur dosage at values slightly higher than zero ("there is no demand for residual SO_ {2} as agent reducer "); the dosed sulfur is therefore used only for halogen consumption inside the boiler, and the agent reducer is, for example, external thiosulfate instead of SO2 residual from the gross boiler gas.

The free chlorine or bromine that bursts into the gas pure when SO2 is missing is determined by direct measurement of Cl 2 or Br 2 content in the pure gas after washing alkaline (for example behind the aspiration shot but, attention, in front of the catalytic bed of SCR arranged, given the case, below), preferably using a measuring cell electrochemistry, such as the company's chemosensor Dräger Sicherheitstechnik (see [8]). The measuring gas is extracted continuously the smoke gas channel through a bypass, dried and then analyzed in the chemosensor. He free chlorine (or free bromine) causes in the measuring cell of the chemosensor a change in tension that becomes a concentration. However, due to the high sensitivity cross section of the sensor against nitrogen oxides (NO x) also contained in pure gas before the SCR, must be corrected constantly measured primary values of Cl_ {2} with respect to the spurious indication of Cl_ {2} attributable to NO_ {x} through the Current content of NO_ {x} in pure gas.

To control the contents of Cl_ {2} or Br 2 in the pure gas after washing the smoke gas (by example behind the aspiration shot but, attention, in front of the SCR catalytic bed arranged, if necessary, below) it could also be placed alternatively, either instead of or in addition to the electrochemical measuring cell, another apparatus for measurement of Cl2 or / and Br2 of continuous detection, by example an apparatus based on infrared spectrometry next.

In the case of chlorine, halogen measurement free that break into the pure gas must be done in front of the SCR catalytic bed, since it has been shown that when the pure gas passes through the SCR free chlorine is transformed back into large part in HCl according to the Deacon reaction for catalyzed chlorine by the SCR catalyst under the conditions of pure gas there present (reduced residual chlorine load, high content of water vapor, approximately 300 ° C). This, however, is not applies to free bromine (Deacon reaction for bromine) or iodine free (Deacon reaction for iodine).

Another possibility to control the supply enough of SO_ {2} would consist, for example, in measuring the hypohalogenide content in sewage from washing alkaline.

As explained, when the flow rate of highly halogenated waste increases sharply, the burden of Halides in the wastewater of the acid wash are delayed with with respect to the total current load of halogens in the smoke gas due to the residence time of the wastewater in the washer circulation / acid washer decanter reservoir.

So, in the case of these sharp increases load, the theoretical SO_ {2} content (either the content of theoretical calculated SO_2 adjusted in the smoke gas in front of the boiler or the residual theoretical SO2 content adjusted directly in the gross boiler gas before cooling abrupt by a measurement of conductivity and amounts in wastewater) does not adapt with sufficient speed to the current total halogen load despite intervention regulator of the primary regulation circuit, so that it may temporarily cause a lack of SO_ {2} and, in consequently, the unwanted irruption of, for example, Cl_ {2} or Br2 free in pure gas after alkaline washing.

To completely avoid the irruptions due at rapid increases in load, the amount of sulfur dosed should be increased on time and temporarily exceeded by, for example, 5 a 100%, preferably 10 to 50%, until the amount of sulfur required by the primary regulation circuit again sufficient alone for the suppression of X_ {2} and the reduction of NaOX.

To make this increase, the content residual of theoretical SO2 in the gross boiler gas before rough cooling is increased through a "circuit of expanded regulation "in up to 1,000 mg of SO2 / Nm3 tr., for example in the case of chlorine from a content of Cl 2 in the pure gas ≥ 0.5 mg of Cl 2 / Nm 3 tr. Y increasingly as the measured Cl2 content increases In the pure gas. In this way it is guaranteed that also in the In case of a sharp increase in the chlorine load, always be present a sufficiently large excess of SO2 in the gas boiler gross before abrupt cooling.

Alternatively, the amount of sulfur it can also be increased excessively when the load starts to rise of halides in acidic wastewater (as an indication that there is a sharp increase in the total load of halogens), preferably proportionally to the velocity at what is observed increases the conductivity.

Both measures, both the possible intervention to cause of the concentration of free halogen in the pure gas after of the flue gas washing as well as the possible intervention to cause of a rapid increase in the halide load in the waters acid residues, can be applied, together or separately, in the "extended regulation circuit".

The process according to the invention for controlled suppression of free halogens you can also apply analogously to discontinuous waste feed ("batch operation mode"). In this case, the Dosage of sulfur and / or other sulfur carriers must engage in batch feeding, that is, increase periodically, and should be done, depending on the content of halogens or halides in the lots, with respect to the magnitude, the time and duration of the corresponding dosing pulse of sulfur.

The dosage of sulfur and / or others Sulfur carriers according to the feeding rate and adapted to the size of the lot in terms of magnitude, timing and duration can be based on individual stored barcodes automatically for the calorific value, the type of halogen and the amount of halogen from the individual batches.

In the case of granulated dosage of sulfur the dosing device is also preferably a Endless dosing screw with pneumatic conveying pipe subsequent directed towards the primary combustion chamber.

If sulfuric acid is dosed waste the sulfur dosing device is preferably a metering pump with nozzle or windshield next through which it is sprayed into the chamber of primary or secondary combustion.

The process according to the invention It has the advantage that by regulated sulfur dosing or other sulfur carriers in the combustion chamber are they eliminate free halogens, such as Cl2 and / or Br2, in no less than two points of the incinerator, namely, on the one hand already in the recovery boiler (direct gas phase reaction with SO2) and on the other in alkaline washing (reduction of hypohalogenides with bisulfide formed from residual SO2 chemo absorbed). Through regulated sulfur dosing proportional to the total variable load of halogens (circuit of primary regulation) and the contribution of a disturbing magnitude with a temporarily excessive amount of sulfur when they burst free halogens in pure gas (extended regulation circuit with contribution of a disturbing magnitude) is guaranteed that by one part covers the minimum sulfur demand and on the other the washing acid or alkaline is not unnecessarily charged with compounds of oxidized sulfur, such as SO 3 / SO 4 2- (acid wash) or SO2 (alkaline wash), respectively. Therefore not there is an unnecessarily high sulfur expenditure and, therefore so much, neither an unnecessarily high alkali expenditure, nor in the alkaline washing (NaOH expenditure) or in water treatment residuals / precipitation of heavy metals willing to continuation (for example Ca (OH) 2) expense, and finally neither an unnecessarily high generation of residual substances to be deposited, such as calcium sulfate dihydrate CaSO 4 x 2 H 2 O.

Bibliography

[1] HW Fabian , P. Reher and M. Schoen "How Bayer incinerates water", Hydrocarbon Processing , April 1979 , pg. 183

[2] RD Griffin "A New Theorie of Dioxin Formation in Municipal Solid Waste Combustion", Chemosphere Vol. 15 ( 1986 ), pgs. 1987-1990

[3] T. Geiger , H. Hagemeiner , E. Hartmann , R. Römer , H. Seifert "Einfluss des Schwefels auf die Dioxin- und Furanbildung bei der Klärschlammverbrennung", VGB Kraftwerktechnik 72 ( 1992 ), pgs. 159-165;

[4] P. Samaras , M. Blumenstock , D. Lenoir , k. W. Schramm , A. Ketttrup "PCDD / F Prevention by Novel Inhibitors: Addition of Inorganic S- and N- Compounds in the Fuel before Combustion", Environ. Sci. Technol . 34 ( 2000 ), pgs. 5092-5096

[5] DA Oberacker , DR Roeck , R. Brzezinski "Incinerating the Pesticide ethylene Dibromid (EDB: a Field-Scale Trial Burn Evaluation Environmental Performance", Report EPA / 600 / D-88/198, Order No. PB89-118243 ( 1988 )

[6] EP 0 406 710

[7] W. Oppenheimer , K. Marcek : "Thermische Entsorgung von Produktionsabfällen", Entsorgungs-Praxis 6 ( 2000 ), pgs. 29-33

[8] Fa. Dräger Sicherheitstechnik: Produkspezifikatzion für DrägerSensor Cl_ {2} - 68 09 725

[9] JP 2000-205525.

Figures and examples

They show:

Figure 1 the scheme of an incinerator of waste (special waste incinerator VA1 in the center of BAYER waste disposal Leverkusen-Bürrig)

Figure 2 the closed balance of sulfur going on by combustion, boiler and acid washing for the incineration of highly chlorinated waste

Figure 3 Chlorine Balance (HCl discharge with the wastewater from the acid wash or discharge of NaCl with sewage from alkaline wash)

Figure 4 a regulation circuit primary

Figure 5 a sulfur dosing ramp for the incineration of highly chlorinated waste

Figure 6 determining a point of the linear sulfur dosing ramp

Figure 7 the sharp increase in total load of halogens in the smoke gas and the delayed increase over this one of the halide load in acidic wastewater

Figure 8 an example of the emergence of Cl_ {2} when the load increases sharply using only the primary regulation circuit

Figure 9 an extended regulation circuit with contribution of a disturbing magnitude

Figure 10 indication correction Cl 2 spurious as a result of transverse sensitivity  versus NO_ {x} of a Cl2 measuring device in the gas pure before the SCR

Figure 11 the application of load jumps of chlorine for the test depicted in figure 12 below using the extended regulation circuit

Figure 12 when using the circuit expanded regulation with the contribution of a disturbing magnitude not Irruption of Cl 2 is observed despite the sharp increase in load

Figure 13 the closed sulfur balance going through combustion, boiler and acid washing for incineration of highly brominated waste

figure 14 the bromine balance (discharge of HBr with sewage in acid wash or NaBr discharge with sewage from alkaline wash)

Figure 15 a comparison of conductivities of aqueous solutions of HCl and HBr

Figure 16 the retroconversion of Cl_ {in} HCl when pure gas crosses the SCR ready to continuation.

Figure 1 shows a waste incinerator typical (in this case it is the waste incinerator Specials VA1 of the waste disposal center of BAYER Leverkusen-Bürrig) with feeding devices for solid waste and lots 1, as well as for liquid waste 2, the rotary tubular furnace 3, the post-combustion chamber 4, the recovery boiler 5, rough cooling 6, the acid rotary washer-sprayer 7, el 8-alkaline rotary washer-sprayer, the EGR of condensation 9, suction shots 10, an installation of SCR 11 denitrification set forth below and the chimney 12.

Figure 2 shows by way of example for the Chlorine case, that is, for the incineration of waste highly  chlorinated, a "closed balance of sulfur under combustion, boiler and acid wash. "This representation provides the evidence that approximately 3% of the total chlorine load, in intermediate Cl2 form, is transformed back into HCl and SO 3 in the boiler via SO 2; the generated SO_ {3} is recovers in the form of SO_4-2 in acidic wastewater of sudden cooling. The operational tests of Figure 2 they were made with a high and constant sulfur intake, increasing the total chlorine load step by step. The abscissa of diagram is the total chlorine load with respect to the gas flow rate of dry smoke and is therefore expressed in mg of Cl_ tot / Nm 3 tr. The ordinate of the diagram is the "mass sulfur flow rate" contained in the SO2 of the gas smoke and / or in the SO4 {2-2} of the wastewater, referred to in each case at a flow rate of smoke gas of approximately 40,000 Nm 3 tr / h in the facility analyzed in this case (mg of S / Nm 3 tr.). Some are also indicated in Figure 2 SO2 values measured after acid washing, that is, in pure gas washed with acid in front of the alkaline scrubber, for demonstrate that the SO_ {2} present in the raw gas (behind the boiler / before abrupt cooling) crosses the washing zone acid as expected.

Figure 3 shows the chlorine balance corresponding, which now includes alkaline washing (alkaline rotary washer-sprayer (LRA)), to demonstrate by way of example that when the sulfur intake is enough, 99% of the total chlorine load comes in the form of HCl when acid washing and only 1% of the total chlorine load comes in the form of Cl 2 to the alkaline wash in which it is finally reduced (to through the residual SO2 in the gross boiler gas before rough cooling) to stable chloride.

Figure 4 shows by way of example for chlorine case the primary regulation circuit using the ramp of sulfur dosage 13 specific for chlorine and adjusting the theoretical residual SO2 value 14a in the gross boiler gas 14 before abrupt cooling depending on the load of halides present in the cooling sewage abrupt, the latter being found from the content of HCl 15 in wastewater (determined by conductivity measurement thermocompensated 16) by multiplication by the water flow residuals 17 (MID measurement). The mass flow dosage required sulfur granulate 18 in the chamber head of primary combustion (rotary tubular furnace) 3 is carried out at through the dosing worm 19 and a pipe pneumatic transport 20. The magnitude of adjustment is the frequency of rotation of the motor member 21 of the dosing screw. This turn frequency is modified through the regulator P-I R.3332 22. This regulator 22 compensates constantly the value of real residual SO_ {14} measured behind of the recovery boiler 5 with the residual SO2 value theoretical 23 required according to the dosing ramp of sulfur 13.

Figure 5 shows, again by way of example for the case of chlorine, the sulfur dosing ramp specific for chlorine previously found in operational tests and used in the primary regulation circuit (figure 4). For its determination, 6 incineration tests were carried out with different total loads. The main parameters of these operational tests are indicated in Table 1. In each of the operational tests the flow rate of a mixture of highly chlorinated liquid wastes consisting of dichloropropane DCP and chlorinated hydrocarbon HCC (with known chlorine contents in each case). The corresponding chlorine charge (based on a mass flow rate of dry smoke gas of approximately 40,000 Nm 3 tr / h) is shown in Figure 5 as an abscissa value; the ordinate in Figure 5 indicates the theoretical residual residual SO2 value required (residual SO2 content
minimum) in the gross boiler gas before sudden cooling with respect to the mass flow of dry smoke gas.

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TABLE 1 Main parameters of the 6 operational tests to find the sulfur dosing ramp in the case of chlorine (VA2 smoke gas flow rate approximately 40,000 Nm 3 tr / h)

one

Figure 6, corresponding to test 4 of the Table 1, shows by way of example the procedure used to find a point on the sulfur dosing ramp. The diagram shows the residual SO_ {2} contents in the gross gas of boiler (ordered left) and free chlorine in pure gas after alkaline wash, measured behind the aspiration shot (ordered right), depending on the test time. At first a high residual SO2 content in the raw gas was chosen boiler, which was slowly reduced at the beginning of the essay. From a residual SO2 content of about 1,400 mg of SO 2 / Nm 3 tr. in the gas boiler gross before abrupt cooling begins to rise slightly the concentration of Cl2 in the pure gas before the SCR until after 12:30 pm, at approximately 500 mg of residual SO 2 / Nm 3 tr., a marked increase occurs of free chlorine (irruption of Cl 2). The content of SO_ {2} residual from which the concentration of Cl 2 in the pure gas and the concentration of Cl_ {tot} corresponding in the smoke gas (in this case approximately 36 g of Cl_ tot / Nm 3 tr) determine a ramp point of sulfur dosage. Other trials show that the ramp Sulfur dosing is really straight.

As Figure 7 shows, which represents the selective sharp increase in the flow of halogens again in the example of chlorine, the halide load found indirectly at from the wastewater of the acid wash is delayed with with respect to the total current load of halogens in the smoke gas Due to the size of the washer mud.

Figure 8 shows the lack of SO 2 caused by this delay as the load increases sharply as a result of the delayed recording of the current total halogen charge, as well as the breakdown of Cl 2, which is still to be observed, in pure gas after alkaline washing when only the primary regulation circuit operates. Once the primary regulation circuit has been put into operation at 1:45 p.m., the primary control circuit first reduces the residual SO 2 content in the raw boiler gas from the previously selected value to the value actually required at this time. according to the sulfur dosing ramp. At 14:35 hours the sharp increase, selectively caused, of the chlorine load of 900 kg / h to 1,400 kg / h (see Figure 7) was carried out. As a result of the delay in the recording of the current total load of chlorine that rises rapidly and, therefore, of the delay in the adjustment of the residual SO2 content occurs after 45 min (16:15 hours) a increase in the concentration of Cl 2 in the pure gas and finally an "irruption of Cl 2" in the pure gas, with values >> 5 mg of Cl 2 / Nm 3 tr. } When the residual SO_ {4} content finally reaches the required final value, the irruption of
Cl_ {2}.

This type of breakthrough of Cl_ {2} can be avoid with the "regulation circuit with input from a disturbing magnitude "extended with respect to the circuit of primary regulation, represented in figure 9. According to the extended regulation concept, the residual value of SO_ {2} theoretical 14a in the gross boiler gas 14 before cooling abrupt is not achieved only by the dosing ramp of sulfur 13 as a function of the delayed chloride load present in acidic wastewater and gradually increasing the amount of 18 sulfur dosed. Rather it increases temporarily and selectively in excess of the theoretical residual SO2 value 14a in the gross boiler gas before abrupt cooling as soon as an increase in free chlorine in pure gas is measured after alkaline wash 8 / behind the aspiration shot 10 (but, attention, before the catalytic bed of SCR ready to continuation). For this measurement of free chlorine is used preferably a chemosensor 25 from Dräger Sicherheitstechnik. The measuring gas is continuously extracted from the Smoke gas channel, dried and analyzed. Free chlorine causes in the chemosensor measuring cell 25 a voltage change that It becomes a concentration. Due to the high sensitivity cross section of sensor 25 against nitrogen oxide NO x 26, still contained in pure gas before the SCR, the primary value of Cl 2 measured in the sensor 25 is corrected with respect to the spurious indication attributable to NO_ {x} with factors of correction 27 specific to the device (calculation of the indication spurious 28, the spurious indication of the measured value is subtracted Cl 2 primary 29).

The spurious indication of Cl_ {2} ΔCl 2 (28) that occurs as a result of the transverse sensitivity to NO x of the measuring cell Dräger 25 installed follows a simple correction equation specific to the apparatus, for example of type ΔCl2 / ppm = a * NO_ {x} / (mg / Nm_ {tr.}). In the case of content occasionally high NOx in the pure gas before the SCR it is recommended, in view of the low limit value of Cl_ {2}, to apply a correction equation of type ΔCl2 / ppm = a '* [(NO_ {x} / (mg / Nm_ {tr.})) 2 -b '* NO_ {x} / (mg / Nm_ {tr.})] And set the coefficients a 'and b' of this correction equation by corresponding operational measurements; these can be effect, for example, directly on the operational smoke gas in a driving mode rich in NO_ {x} but chlorine free (results of the measurements in figure 10).

As Figure 9 also shows, the value of Cl_ {2} measured and corrected for NO_ {x} becomes, from a pre-selectable Cl 2 content in pure gas of, for example, 0.5 mg of Cl 2 / Nm 3 tr., by the regulator R.3401 31 in an additional demand for SO_ {2} than in the amplifier 32 can be multiplied again by a factor of pre-selectable amplification 33 of, for example, 10. This demand additional SO2 is added in the "apparatus for adding disturbing quantities "34 to the demand of SO_ {2} of the primary regulation circuit. Thus, the theoretical SO_ {2} value 23 increases by, for example, 1,000 mg of SO 2 / Nm 3 tr. The regulator 22 constantly compensates again for the value of Real residual SO_ {2} measured behind the recovery boiler 5 with the theoretical residual SO 2 value 23 increased by according to the contribution of disturbing quantities described.

This ensures that there is always a contribution of SO_ {2} large enough when it increases abruptly the load of chlorine.

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As a redundant security measure against Irruptions of Cl_ {2} can also be used to increase Temporary load of chlorides in sewage sudden cooling, for example through an element DIF differentiator of the regulation technique (differentiation of temporary increase 24), to also increase from here in excess the theoretical residual SO_2 value 23 in the case of rapid rise.

All measures to temporarily increase the theoretical residual SO_2 value 23 beyond the value of SO_ {2} theoretical residual demanded late only by the Sulfur dosing ramp 13 can be used together (addition in the addition device of disturbing quantities 34) or by separated.

In order to demonstrate the effect of the extended regulation circuit with the contribution of disturbing quantities, large jumps in the total chlorine load were selectively again carried out in another operational test, see figure 11. Despite the strong and rapid load changes shown in the figure 11, the expanded regulation circuit (Figure 9) provided the excellent result shown in Figure 12: When the expanded regulation circuit is put into operation at 12:40 hours, the residual SO 2 content first decreases again to a value of approximately 1,200 mg of SO 2 / Nm 3 tr. corresponding to the total chlorine load according to the sulfur dosing ramp. After reducing the chlorine load of 1,500 kg / h to 1,100 kg / h at 13:10 hours, the residual SO2 content in the raw boiler gas continues to decrease. At 14:30 hours the chlorine load is sharply increased. Due to the appearance of free chlorine> 0.5 mg / Nm 3 tr. In the pure gas, an excessive excessive increase in the value of SO_ is produced through the R.3401 regulator (see Figure 9). 2 theoretical residual and, consequently, a rapid increase in the real residual SO2 content in the raw boiler gas before abrupt cooling by approximately 1,000 mg SO2 / Nm3 tr. } Consequently there is no break in Cl 2, instead the Cl 2 content in the pure gas immediately returns to values <0.5 mg / Nm 3 tr. Note: At 4:10 p.m. there was a brief failure in the sulfur metering screw: as a consequence, the residual SO2 content was temporarily reduced to very low levels, so that pure gas was obtained again a small peak of free chlorine (16:15 hours). Thus, as response of the extended regulation circuit to strong load jumps comparable to the previous ones, they are only detected, unlike in the primary regulation circuit only (see Figure 4), extremely small Cl2 peaks included in a range of
concentration << 5 mg Cl 2 / Nm 3 tr.

The examples described so far are limited essentially to the incineration of residues with chlorine content. However, as evidenced by the closed sulfur balance for bromine in figure 13 as well as the bromine balance in figure 14, the basic relationships found above for the example of Chlorine are also applicable in principle to other halogens, as bromine can be, which is considered another example, although much higher proportions of free halogens are involved.

Similarly to figure 2 for the case of Chlorine Figure 13 shows in the case of bromine that in the boiler an average proportion of Br2 of approximately 61% of the total bromine charge (instead of 3% in the case of chlorine). Note: Bromine-rich liquid waste incinerated in the test they also contained, in addition to 25% bromine, approximately 3% of chlorine; this chlorine has been taken into account in figure 13, that is, that the represented result of the valuation is "clean of chlorine".

Similarly to Figure 3 for the case of chlorine figure 14 shows for the case of bromine which also in this case only reaches approximately 1% of the alkaline wash total load, that is, despite the proportion much more high free bromine in the total bromine load is separated 99% of the total bromine load in the acid wash if the contribution of Sulfur is enough.

Finally, figure 15 shows the comparison of the conductivities (thermocompensated at 20ºC) of solutions aqueous HCl and HBr. When they have the same conductivity the bromide mass content is more than twice the content chloride mass, corresponding to a mass ratio Molecular HBr / HCl = 80,948 / 36,465 = 2.22.

Many highly chlorinated liquid residues do not They contain bromine or contain only little bromine. Most of the highly brominated liquid waste instead, also contain, In addition to bromine, notable amounts of chlorine. In the case of these residues rich in bromine and at the same time rich in chlorine can be start, when assessing conductivity measurements, only from, for example, bromine (as the main halogen) without make noteworthy mistakes in the subsequent calculation of the sulfur demand, that is, based solely on the curve of conductivity of aqueous bromide solutions, provided that in the Next calculation of the sulfur demand is also split only from bromide, that is, the corresponding molecular mass of HBr is used. Thus, instead of the amount of chloride present simultaneously it is in the valuation of the measured values of conductivity an "amount of bromide equivalent" to the sulfur demand.

Finally, figure 16 demonstrates the fact noted several times before that when pure gas goes through a SCR of pure gas arranged then the chlorine free is largely transformed back into HCl according to the Deacon reaction for chlorine catalyzed by SCR catalyst rich in metal oxides in the conditions of pure gas there present (reduced residual chlorine load, high content in water vapor, approximately 300 ° C).

Claims (25)

1. Procedure for the low corrosive and poor co-incineration of highly halogenated liquid waste in waste incinerators, in which the waste incinerator contains at least one combustion chamber (3), a recovery boiler (5), a washing of multi-stage smoke gas formed by an acid wash (7) and an alkaline wash (8), characterized in that sulfur or a suitable sulfur carrier is dosed in a regulated manner depending on the total load of halogens and halogen type. 2. Method according to claim 1, characterized in that the amount of sulfur is dosed in a regulated manner and proportional to the current total load of chlorine, bromine or iodine in the waste. 3. Method according to claims 1 and 2, characterized in that the amount of sulfur is dosed in a regulated manner according to an operationally determined sulfur dosing ramp and which establishes for SO corresponding residues rich in chlorine, bromine or iodine the content of SO_ {2} residual in the raw gas behind the boiler (before abrupt cooling) necessary for the current total halogen load. 4. Method according to claims 1 to 3, characterized in that the linear sulfur dosing ramp is operationally available for the corresponding residues rich in chlorine, bromine or iodine, determining, for at least a greater load of chlorine, bromine or iodine in the residues , the minimum SO 2 content required in the raw boiler gas that in the steady state of operation does not allow the detection of free chlorine, bromine or iodine or only an amount less than a predetermined limit value in the pure gas after washing the gas from
smoke. 5. Method according to claims 1 to 4, characterized in that the current total halogen charge present in the smoke gas is continuously determined approximately as a halide charge in the wastewater of the acid scrubbing of the smoke gas, that is, as product of the halide concentration and wastewater flow. Method according to one of claims 1 to 4, characterized in that the current total halogen load present in the smoke gas is determined continuously by measuring the halogen and hydrogen halide species in the raw boiler gas before cooling. abrupt (behind the boiler) and from the flow of dry smoke gas or a magnitude proportional to the flow of smoke gas, such as the specific vaporization of the
boiler. Method according to one of claims 1 to 6, characterized in that the amount of sulfur corresponding to the total halogen charge in the smoke gas and / or the halide charge in the wastewater of the acid wash according to the ramp The sulfur dosage is briefly increased by an excess of 5 to 100%, preferably 10 to 50%, as soon as chlorine, bromine or free iodine is measured in the pure gas after washing the smoke gas, but in front of the catalytic bed SCR provided, if necessary, below. Method according to one of claims 1 to 6, characterized in that the amount of sulfur corresponding to the total halogen charge in the smoke gas or the halide charge in the wastewater of the acid wash according to the dosing ramp Sulfur is briefly increased by 5 to 100%, preferably 10 to 50%, as soon as a rapid rise in the halide concentration is detected in the wastewater of the acid wash. Method according to one of claims 1 to 8, characterized in that the sulfur is added in the form of solid sulfur, liquid sulfur or waste sulfuric acid. Method according to one of claims 1 to 9, characterized in that solid sulfur is dosed in pelletized or granulated form through adjustable dosing organs. Method according to one of claims 1 to 10, characterized in that the solid sulfur is fed into the primary combustion chamber by pneumatic transport. 12. A method according to one of claims 1 to 9, characterized in that the sulfuric acid is discharged into the primary or secondary combustion chamber by means of adjustable metering pumps. 13. Method according to one of claims 1 to 9 or 12, characterized in that the waste sulfuric acid is fed into the primary or secondary combustion chamber through a spray nozzle or corresponding windshield. 14. Method according to one of claims 1 to 13, characterized in that in the case of a total halogen charge that varies periodically in the smoke gas as a result of the pulse feeding of individual lots rich in halogens, a sulfur dosage is produced. and / or other sulfur carriers according to the feeding rate and adapted to the size of the lot in terms of magnitude, timing and duration. 15. Method according to claim 14, characterized in that the dosage of sulfur and / or other sulfur carriers according to the feed rate and adapted to the size of the batch in terms of magnitude, timing and duration is based on codes of Individual bars automatically stored for the calorific value, the type of halogen and the amount of halogen present in the lots. 16. Method according to one of claims 1 to 15, characterized in that the reduction of hypohalogenides is carried out in the alkaline wash by means of the bisulfide formed in the process from the residual SO2 of the raw boiler gas and simultaneously or only by means of a external reducing agent such as thiosulfate. 17. Method according to one of claims 3 to 16, characterized in that an operationally determined sulfur dosing ramp is also used for chlorine-only residues for the incineration of halogen mixtures containing other halogens in addition to chlorine. 18. Waste incinerator with a combustion chamber (3), a recovery boiler (5), a multi-stage smoke gas wash consisting of an acid wash (7) and an alkaline wash (8), which contains regulating devices for regulated dosing of sulfur and / or other sulfur carriers in the primary or secondary combustion chamber (3), (4), characterized in that the regulating device is composed of a primary regulation circuit with adjustment of the theoretical value of the content of residual SO2 continuously measured in the raw boiler gas before abrupt cooling or of a corresponding expanded regulation circuit with additional input of disturbing quantities and in which the primary regulation circuit regulates the sulfur dosage according to a Sulfur dosing ramp proportional to the current total halogen load in the smoke gas or to the halide load in acidic and functional wastewater n-type halogen. 19. Waste incinerator according to claim 18, characterized in that the regulating device is composed of a primary regulation circuit with adjustment of the theoretical value of the SO2 content calculated in line in the smoke gas in front of the boiler or of a corresponding expanded regulation circuit with an additional contribution of disturbing quantities, in which the primary regulation circuit regulates the sulfur dosage proportionally to the current total halogen load in the smoke gas or to the halide load in the wastewater acids by continuously calculating the specific degree of transformation for the halogen and by the frequency of rotation of the dosing equipment, taking into account the static transport characteristic of the dosing equipment. 20. Waste incinerator according to claim 18 or 19, characterized in that the corresponding expanded regulation circuit temporarily increases the sulfur dosage (contribution of disturbing quantities) excessively when Cl 2 begins to break into the pure gas and / or when The halide content in acidic wastewater rises rapidly. 21. Waste incinerator according to one of claims 18 to 20, characterized in that a sulfur dosing ramp according to claim 4 is used in the control circuit. 22. Waste incinerator according to one of claims 18 to 21, characterized in that the current halogen charge is determined according to one of claims 5 or 6. 23. Waste incinerator according to one of claims 18 to 22, characterized in that it contains dosing equipment and conveyor equipment for regulated dosing of sulfur or other sulfur carriers in the primary or secondary combustion chamber (3), (4). 24. Waste incinerator according to claim 23, characterized in that the equipment for regulated dosing of sulfur or other sulfur carriers is an adjustable conveying equipment, such as a vibrating feeder or an endless dosing screw (19). 25. Waste incinerator according to claim 24, characterized in that the equipment for the regulated dosing of the sulfuric acid waste is an adjustable dosing pump and is sprayed through a nozzle and / or an windscreen in the primary or secondary combustion chamber ( 3. 4).